EP0742283A2 - Apparatus and method of cleaning vapour condensate produced during the boiling of the wort in the beer production - Google Patents

Apparatus and method of cleaning vapour condensate produced during the boiling of the wort in the beer production Download PDF

Info

Publication number
EP0742283A2
EP0742283A2 EP96107490A EP96107490A EP0742283A2 EP 0742283 A2 EP0742283 A2 EP 0742283A2 EP 96107490 A EP96107490 A EP 96107490A EP 96107490 A EP96107490 A EP 96107490A EP 0742283 A2 EP0742283 A2 EP 0742283A2
Authority
EP
European Patent Office
Prior art keywords
module
permeate
semipermeable membrane
pressure
concentrate
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Granted
Application number
EP96107490A
Other languages
German (de)
French (fr)
Other versions
EP0742283B1 (en
EP0742283A3 (en
Inventor
Bernhard Lenz
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Hrch Huppmann GmbH
Original Assignee
Individual
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Individual filed Critical Individual
Publication of EP0742283A2 publication Critical patent/EP0742283A2/en
Publication of EP0742283A3 publication Critical patent/EP0742283A3/en
Application granted granted Critical
Publication of EP0742283B1 publication Critical patent/EP0742283B1/en
Anticipated expiration legal-status Critical
Expired - Lifetime legal-status Critical Current

Links

Images

Classifications

    • C—CHEMISTRY; METALLURGY
    • C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
    • C12C—BEER; PREPARATION OF BEER BY FERMENTATION; PREPARATION OF MALT FOR MAKING BEER; PREPARATION OF HOPS FOR MAKING BEER
    • C12C5/00—Other raw materials for the preparation of beer
    • C12C5/002—Brewing water
    • C—CHEMISTRY; METALLURGY
    • C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
    • C12C—BEER; PREPARATION OF BEER BY FERMENTATION; PREPARATION OF MALT FOR MAKING BEER; PREPARATION OF HOPS FOR MAKING BEER
    • C12C13/00—Brewing devices, not covered by a single group of C12C1/00 - C12C12/04

Definitions

  • the invention relates to a system and a method for cleaning vapor condensates obtained in beer production.
  • the wort obtained by clarifying the mash and then washing the spent grains is cooked in a wort pan.
  • the desired wort concentration is to be achieved by evaporating excess water, in addition to a number of other procedural effects.
  • the vapors formed are usually condensed in a special heat exchanger, for example a pan vapor condenser, the heat inherent in the vapors being able to be recovered to a considerable extent.
  • the condensate accumulating in the ladle vapor condenser contains a number of particularly organic constituents, for example phenyl and benzyl ethanol, 2- and 3-methyl-butanal and butanol, pentanol, hexanol, N-heterocycles, strain gauges and polyphenols, which reuse this condensate, in particular as brewing water , but also as process water, for example boiler feed water or the like. Therefore, the condensate accumulating in the ladle vapor condenser is usually discharged directly or indirectly into the sewage system. Since these condensates are produced in large quantities and the wastewater charges are calculated based on the amount of condensate discharged, the discharge of these condensates into the wastewater system represents a considerable cost factor. Moreover, discarding such wastewater quantities is not environmentally friendly.
  • the condensate to be cleaned is fed to the semipermeable membrane of an RO module (reverse osmosis module) by means of a pressure pump under high pressure, whereby due to the pressure, which must be higher than the osmotic pressure of the condensate, almost pure water diffuses through the semipermeable membrane and can be derived as permeate.
  • the pressure or the operating pressure of the condensate is preferably between 30 and 60 bar, in particular approximately 40 bar. With increasing pressure, the permeability of the membrane for water increases, whereas the permeability for the substances that are retained should remain approximately constant.
  • the concentrate held off by the semipermeable membrane is discharged directly into the sewage system or else initially stored in a buffer store or the like.
  • the system according to the invention has at least one pressure pump for pressurizing the vapor condensate to be cleaned and an RO module having a semipermeable membrane, through which the vapor condensate can be conveyed by means of the pressure pump with separation into permeate and concentrate. Furthermore, according to the invention, at least one drain line for the concentrate for indirect or direct discharge into the sewage system is provided. The cleaned permeate can be collected for reuse.
  • the condensates coming from the ladle vapor condenser can be fed directly to the pressure pump.
  • a reservoir is first arranged between the pressure pump and the ladle vapor condenser, which serves for the intermediate storage of the vapor condensate to be cleaned.
  • this storage container can act in particular as a buffer store, whereby continuous operation of the system according to the invention is possible.
  • a feed pump is preferably arranged between the feed tank and the pressure pump to convey the vapor condensate to be cleaned from the feed tank.
  • This feed pump only has a transport function. A pressure increase to the operating pressure of the RO module is not brought about by this feed pump.
  • a collecting container is arranged on the permeate discharge side of the RO module, which serves to hold the permeate that has passed through the semipermeable membrane.
  • this collecting container serves in particular to ensure continuous operation of the entire system.
  • an activated carbon filter unit through which the permeate can flow can be arranged on the permeate discharge side of the RO module. This activated carbon filter unit only functions as a safety device.
  • a pressure booster pump for the permeate is therefore arranged on the permeate discharge side of the RO module, which serves on the one hand to transport the permeate and to introduce the permeate into a line system and on the other hand to promote the permeate through the activated carbon filter unit.
  • the pressure is increased to permeate pressure values between 3 and 10 bar, in particular approximately 5 bar.
  • the cleaning efficiency of the system according to the invention depends, among other things, very significantly on the permissible operating pressure of the RO module. Basically, the higher the operating pressure applied by the pressure pump, the higher the permeate yield. However, this permissible pressure is limited overall by the mechanical properties of the semipermeable membrane and the RO module. In order to nevertheless increase the overall efficiency of the cleaning system according to the invention or of the method according to the invention, according to a particularly preferred exemplary embodiment of the invention, a switchable return line for the concentrate retained by the semipermeable membrane and exiting from the RO module is in front of the pressure pump for renewed flow through the RO Module provided.
  • Multiple cleaning of the concentrate is also possible according to the invention in that a plurality of RO modules are connected in series in a simple manner so that the concentrate drain from an upstream RO module opens directly or indirectly into a downstream RO module, the concentrate there is again subjected to a cleaning process.
  • a so-called fir tree arrangement of a plurality of RO modules is advantageous in particular in larger systems, that is to say systems in which larger amounts of vapor condensates are to be worked up or cleaned according to the invention.
  • at least two, but preferably four or more, RO modules are initially arranged in parallel in a first stage, and are passed through by the vapor condensate stream by dividing it.
  • the concentrate drains of the RO modules of this first stage can then be combined and fed to one or more RO modules of a second stage for further or renewed cleaning, etc.
  • the number of stages ultimately depends on the one hand on the amount of vapor condensate to be cleaned or thus the number of RO modules of the first stage and on the other hand the desired degree of cleaning or efficiency of the entire system.
  • a simple and reliable design of the system according to the invention is thus possible.
  • the type of semipermeable membrane is used in the system according to the invention or in the method according to the invention depends in particular on the type of organic impurities to be removed.
  • the characteristic factors are in particular the molecular weight, the molecular size, the spatial structure and the ionogenicity of the molecules of the impurities.
  • a highly crosslinked aromatic polyamide composite membrane Such a membrane is typically used for sea water desalination, for example.
  • a spiral wound winding module is preferably used as the actual RO module, which has a textile carrier which carries the actual semipermeable membrane. This design offers, in a manner known per se, in particular sufficient mechanical strength of the RO module for operating pressures in the range up to 70 bar and more.
  • the plant and method according to the invention are also suitable in the brewery area, inter alia, for the cleaning and treatment of the water obtained in the CO 2 scrubber from the pre-scrubber.
  • the system according to the invention shown in FIG. 1 first of all has an inlet 1 for the vapor condensate originating from a ladle vapor condenser, not shown.
  • the inlet 1 opens into a storage container 2, in which the condensate to be cleaned is initially stored.
  • the storage container 2 can in particular fulfill the function of a buffer store in order to ensure continuous operation of the system according to the invention.
  • the vapor condensate to be cleaned is conveyed from the reservoir 2 to the pressure pump 4 by means of a feed pump 3.
  • the pressure generated by the feed pump 3 need only be so high that a safe transport of the vapor condensate to be cleaned to the pressure pump 4 is ensured.
  • the pressure pump 4 By means of the pressure pump 4, the pressure of the vapor condensate to be cleaned is brought to the operating pressure necessary for the operation of the RO module 5, which is generally between 30 and 60 bar, in particular 40 bar in the exemplary embodiment shown.
  • the semipermeable membrane 6 divides the RO module schematically into two chambers 7 and 8, the chamber 8 with water or the permeate, ie. H. with a liquid of low concentration, in particular organic contaminants, and the chamber 7 with the vapor condensate to be cleaned, i.e. H. a liquid with a relatively high concentration of organic impurities. Due to the pressure applied by the pressure pump 4, the water components of the condensate diffuse from the chamber 7 through the semipermeable membrane 6 into the chamber 8.
  • the permeate thus obtained i. H. more or less pure water, a collection container 9 supplied.
  • the permeate is transported and stored almost without pressure.
  • a pressure booster pump 10 the permeate is conveyed from the collecting container 9 to an activated carbon filter unit 11 and through it, this activated carbon filter unit 11 essentially representing more or less merely a safety device for impurities not retained in the semi-permeable membrane 6.
  • the pressure booster pump 10 serves on the one hand to convey the permeate through the activated carbon filter unit 11 and on the other hand to increase the pressure of the permeate to a value with which this permeate can be fed into a corresponding line system.
  • the filtering process and feeding the permeate into one Line systems are preferably carried out under a pressure between 2 and 10 bar, in particular at about 5 bar.
  • the concentrate i.e. H. essentially the components of the vapor condensate containing the organic impurities are discharged from the chamber 7 of the RO module via a drain line 13.
  • the concentrate can be discharged directly into a sewer system 14, which is only shown schematically.
  • the system has a return line 15 for the concentrate.
  • This return line 15 branches off from the outlet 13 and can be switched on or off by means of valve devices (not shown).
  • the return line 15 opens between the feed pump 3 and the pressure pump 4 in the flow of the condensate to be cleaned and can be switched on or off there by means of valve devices, also not shown.
  • FIG. 2 The exemplary embodiment of an installation according to the invention for cleaning vapor condensates shown in FIG. 2 corresponds in its basic structure to the installation according to FIG. 1 .
  • the singular RO module of the system according to FIG. 1 is, however, replaced by a fir tree-like arrangement 23 of seven essentially identical RO modules 16, 17, 18, 19, 20, 21 and 22, which are arranged in three in succession, based on the flow direction of the condensate to be cleaned, placed stages I, II and III are arranged.
  • the first stage I has four RO modules 16, 17, 18 and 19 arranged in parallel next to one another, on which the flow of the vapor condensates conveyed by the pressure pump 4 is based distributed. This alone increases the capacity of the entire system, which is essentially determined by the flow rate of the RO modules, compared to the system according to FIG. 1 .
  • the second stage II two RO modules 20, 21 are also arranged side by side in parallel.
  • the concentrate drains of the RO modules 16, 17 and 18, 19 of the first stage I open directly into the RO module 20 and 21 of the second stage II, where they are subjected to a renewed cleaning or filtering process.
  • the concentrate drains of the RO modules 20, 21 of the second stage II open into the RO module 22 of the third stage III.
  • the concentrate is finally discharged via the line 13 into the sewage system 14 or, if desired, again via the return line 15 for further cleaning into the RO module arrangement 23.
  • the permeate passing through the RO modules is in each case passed directly via the activated carbon filter unit into the collection container for further use, for example as brewing water. With this fir tree-like RO module arrangement 23, a high cleaning efficiency of the system can be achieved in a simple and easy manner.

Landscapes

  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Engineering & Computer Science (AREA)
  • General Health & Medical Sciences (AREA)
  • Food Science & Technology (AREA)
  • Biochemistry (AREA)
  • Bioinformatics & Cheminformatics (AREA)
  • General Engineering & Computer Science (AREA)
  • Health & Medical Sciences (AREA)
  • Genetics & Genomics (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Wood Science & Technology (AREA)
  • Zoology (AREA)
  • Separation Using Semi-Permeable Membranes (AREA)
  • Cleaning By Liquid Or Steam (AREA)
  • Detergent Compositions (AREA)
  • Water Treatment By Sorption (AREA)
  • Distillation Of Fermentation Liquor, Processing Of Alcohols, Vinegar And Beer (AREA)

Abstract

An appts. and process for purification of condensated obtd. by condensn. of the vapours evolved during cooking of the wort during the prodn. of beer, comprises a pump to pump the condensate under pressure through a reverse osmosis unit contg. semipermeable membrane in which the condensate is sepd. into a permeate which is collected for further use and a concentrate which is led off for direct or indirect disposal into the drains. The semipermeable membrane is pref. of highly crosslinked aromatic polyamide and the reverse osmosis module is pref. a spirally wound module with a textile carrier and the actual semipermeable membrane.

Description

Die Erfindung betrifft eine Anlage und ein Verfahren zur Reinigung von bei der Bierherstellung anfallenden Brüdenkondensaten.The invention relates to a system and a method for cleaning vapor condensates obtained in beer production.

Bei der Bierherstellung wird die durch Abläutern der Maische und das anschließende Auswaschen der Treber gewonnene Würze in einer Würzepfanne gekocht. In diesem Kochvorgang soll neben einer Reihe anderer verfahrenstechnischer Wirkungen die gewünschte Würzekonzentration durch Verdampfen überschüssigen Wassers erzielt werden. Die dabei entstehenden Brüden werden üblicherweise in einem speziellen Wärmetauscher, z.B. einem Pfannendunstkondensator, kondensiert, wobei die den Brüden innewohnende Wärme zu einem erheblichen Anteil zurückgewonnen werden kann. Das im Pfannendunstkondensator anfallende Kondensat enthält eine Reihe insbesondere organischer Bestandteile, beispielsweise Phenyl- und Benzylethanol, 2- und 3-Methyl-Butanal und -Butanol, Pentanol, Hexanol, N-Heterocyklen, DMS und Polyphenole, die eine Wiederverwendung dieses Kondensates insbesondere als Brauwasser, aber auch als Betriebswasser, beispielsweise Kesselspeisewasser oder dergleichen, ausschließen. Daher wird üblicherweise das im Pfannendunstkondensator anfallende Kondensat mittelbar oder unmittelbar in die Kanalisation abgeleitet. Da diese Kondensate in erheblichen Mengen anfallen und die Abwassergebühren nach der eingeleiteten Kondensatmenge berechnet werden, stellt die Ableitung dieser Kondensate in das Abwassersystem einen erheblichen Kostenfaktor dar. Das Verwerfen derartiger Abwassermengen ist zudem ökologisch nicht unbedenklich.In beer production, the wort obtained by clarifying the mash and then washing the spent grains is cooked in a wort pan. In this cooking process, the desired wort concentration is to be achieved by evaporating excess water, in addition to a number of other procedural effects. The vapors formed are usually condensed in a special heat exchanger, for example a pan vapor condenser, the heat inherent in the vapors being able to be recovered to a considerable extent. The condensate accumulating in the ladle vapor condenser contains a number of particularly organic constituents, for example phenyl and benzyl ethanol, 2- and 3-methyl-butanal and butanol, pentanol, hexanol, N-heterocycles, strain gauges and polyphenols, which reuse this condensate, in particular as brewing water , but also as process water, for example boiler feed water or the like. Therefore, the condensate accumulating in the ladle vapor condenser is usually discharged directly or indirectly into the sewage system. Since these condensates are produced in large quantities and the wastewater charges are calculated based on the amount of condensate discharged, the discharge of these condensates into the wastewater system represents a considerable cost factor. Moreover, discarding such wastewater quantities is not environmentally friendly.

Weiter fallen bei der Bierherstellung beispielsweise Brüdenkondensate aus der mechanischen Brüdenverdichtung sowie Mischkondensate, beispielsweise aus der thermischen Brüdenverdichtung, an. Auch diese Kondensate werden üblicherweise in die Kanalisation abgeleitet.Vapor condensates from mechanical vapor compression and mixed condensates, for example from thermal vapor compression, are also obtained in beer production. These condensates are also usually drained into the sewage system.

Ausgehend von diesem Stand der Technik ist es die Aufgabe der vorliegenden Erfindung, eine Vorrichtung und ein Verfahren zur Behandlung von bei der Bierherstellung anfallenden Brüdenkondensaten zu liefern, wodurch die in die Kanalisation abzugebenden Abwassermengen erheblich reduzierbar sind.Starting from this prior art, it is the object of the present invention to provide an apparatus and a method for treating vapor condensates obtained in the production of beer, as a result of which the amounts of waste water to be discharged into the sewage system can be reduced considerably.

Diese Aufgabe wird durch eine Vorrichtung nach der Lehre des Anspruchs 1 und durch ein Verfahren nach der Lehre des Anspruchs 14 gelöst.This object is achieved by a device according to the teaching of claim 1 and by a method according to the teaching of claim 14.

Vorteilhafte Ausgestaltungen der Erfindung sind Gegenstand der Unteransprüche.Advantageous embodiments of the invention are the subject of the dependent claims.

Es ist also zunächst die grundlegende Idee der vorliegenden Erfindung, die anfallenden Brüdenkondensate dergestalt zu reinigen, daß zumindest ein erheblicher Anteil des so gereinigten Abwassers zumindest als Betriebswasser, beispielsweise Kesselspeisewasser, vorzugsweise jedoch als Brauwasser in der Brauerei wiederverwendet werden kann. Da die in den Brüdenkondensaten gelösten, insbesondere organischen, Bestandteile durch ein herkömmliches Filterverfahren nicht oder nicht im gewünschten Umfang aus dem Kondensat ausgeschieden werden können, wird erfindungsgemäß das zu reinigende Brüdenkondensat einem Umkehr-Osmose-Vorgang unterzogen. Dabei wird das zu reinigende Kondensat mittels einer Druckpumpe unter hohem Druck an die semipermeable Membran eines RO-Moduls (Reverse Osmosis-Moduls) geführt, wobei aufgrund des Druckes, der in jedem Fall höher als der osmotische Druck des Kondensates sein muß, nahezu reines Wasser durch die semipermeable Membran hindurchdiffundiert und als Permeat ableitbar ist. Der Druck bzw. der Betriebsdruck des Kondensates beträgt dabei vorzugsweise zwischen 30 und 60 bar, insbesondere in etwa 40 bar. Mit zunehmendem Druck steigt dabei die Permeabilität der Membran für Wasser, wohingegen die Durchlässigkeit für die Substanzen, die zurückgehalten werden sollen, in etwa konstant bleibt. Das durch die semipermeable Membran abgehaltene Konzentrat wird erfindungsgemäß unmittelbar in die Kanalisation abgeleitet oder aber zunächst in einem Zwischenspeicher oder dergleichen gespeichert.It is therefore initially the basic idea of the present invention to purify the vapor condensates obtained in such a way that at least a considerable proportion of the wastewater purified in this way can be reused at least as process water, for example boiler feed water, but preferably as brewing water in the brewery. Since the dissolved, in particular organic, constituents in the vapor condensates cannot be separated from the condensate by the conventional filter process or cannot be removed to the desired extent, the vapor condensate to be cleaned is subjected to a reverse osmosis process according to the invention. The condensate to be cleaned is fed to the semipermeable membrane of an RO module (reverse osmosis module) by means of a pressure pump under high pressure, whereby due to the pressure, which must be higher than the osmotic pressure of the condensate, almost pure water diffuses through the semipermeable membrane and can be derived as permeate. The pressure or the operating pressure of the condensate is preferably between 30 and 60 bar, in particular approximately 40 bar. With increasing pressure, the permeability of the membrane for water increases, whereas the permeability for the substances that are retained should remain approximately constant. According to the invention, the concentrate held off by the semipermeable membrane is discharged directly into the sewage system or else initially stored in a buffer store or the like.

Die erfindungsgemäße Anlage weist mindestens eine Druckpumpe zur Druckbeaufschlagung des zu reinigenden Brüdenkondensates und ein eine semipermeable Membran aufweisendes RO-Modul, durch das das Brüdenkondensat mittels der Druckpumpe unter Trennung in Permeat und Konzentrat förderbar ist, auf. Ferner sind erfindungsgemäß mindestens eine Ablaufleitung für das Konzentrat zur mittelbaren oder unmittelbaren Ableitung in die Kanalisation vorgesehen. Das gereinigte Permeat ist zur Wiederverwendung sammelbar.The system according to the invention has at least one pressure pump for pressurizing the vapor condensate to be cleaned and an RO module having a semipermeable membrane, through which the vapor condensate can be conveyed by means of the pressure pump with separation into permeate and concentrate. Furthermore, according to the invention, at least one drain line for the concentrate for indirect or direct discharge into the sewage system is provided. The cleaned permeate can be collected for reuse.

In grundsätzlich beliebiger Weise können die beispielsweise vom Pfannendunstkondensator kommenden Kondensate unmittelbar der Druckpumpe zugeleitet werden. Nach einem bevorzugten Ausführungsbeispiel der Erfindung jedoch wird zunächst einmal zwischen der Druckpumpe und dem Pfannendunstkondensator ein Vorlagebehälter angeordnet, der zur Zwischenspeicherung des zu reinigenden Brüdenkondensates dient. Dabei kann dieser Vorlagebehälter insbesondere als Pufferspeicher agieren, wodurch ein kontinuierlicher Betrieb der erfindungsgemäßen Anlage möglich ist.In principle, the condensates coming from the ladle vapor condenser, for example, can be fed directly to the pressure pump. According to a preferred embodiment of the invention, however, a reservoir is first arranged between the pressure pump and the ladle vapor condenser, which serves for the intermediate storage of the vapor condensate to be cleaned. In this case, this storage container can act in particular as a buffer store, whereby continuous operation of the system according to the invention is possible.

Zur Förderung des zu reinigenden Brüdenkondensates aus dem Vorlagebehälter ist vorzugsweise zwischen dem Vorlagebehälter und der Druckpumpe eine Vorlagepumpe angeordnet. Diese Vorlagepumpe weist dabei ausschließlich Transportfunktion auf. Eine Druckerhöhung auf den Betriebsdruck des RO-Moduls wird durch diese Vorlagepumpe nicht bewirkt.A feed pump is preferably arranged between the feed tank and the pressure pump to convey the vapor condensate to be cleaned from the feed tank. This feed pump only has a transport function. A pressure increase to the operating pressure of the RO module is not brought about by this feed pump.

Gemäß einem Ausführungsbeispiel ist auf der Permeatablaufseite des RO-Moduls ein Sammelbehälter angeordnet, der zur Aufnahme des durch die semipermeable Membran hindurchgetretenen Permeates dient. Wenngleich auch hier in grundsätzlich beliebiger Weise eine unmittelbare Wiederverwendung des Permeates möglich wäre, dient dieser Sammelbehälter insbesondere dazu, einen kontinuierlichen Betrieb der gesamten Anlage zu gewährleisten.According to one embodiment, a collecting container is arranged on the permeate discharge side of the RO module, which serves to hold the permeate that has passed through the semipermeable membrane. Although direct reuse of the permeate would also be possible here in any way, this collecting container serves in particular to ensure continuous operation of the entire system.

Bestimmungsgemäß werden im RO-Modul praktisch alle organischen Verunreinigungen abgesondert, die die Verwendung des Permeates als Betriebswasser beeinträchtigen könnten. Um jedoch dennoch möglicherweise durch die semipermeable Membran hindurchgetretene Verunreinigungen zuverlässig auszufiltern, kann nach einem weiteren Ausführungsbeispiel der Erfindung auf der Permeatablaufseite des RO-Moduls eine vom Permeat durchströmbare Aktivkohle-Filtereinheit angeordnet sein. Diese Aktivkohle-Filtereinheit fungiert dabei lediglich als Sicherheitsvorrichtung.As intended, practically all organic impurities that could impair the use of the permeate as process water are separated in the RO module. However, in order to reliably filter out any contaminants that may have passed through the semipermeable membrane, an activated carbon filter unit through which the permeate can flow can be arranged on the permeate discharge side of the RO module. This activated carbon filter unit only functions as a safety device.

Während auf der Konzentrat- bzw. Kondensatseite des RO-Moduls der volle durch die Druckpumpe aufgebrachte Betriebsdruck herrscht, tritt das Permeat nahezu drucklos aus dem RO-Modul aus. Ebenso erfolgt gegebenenfalls die Speicherung des Permeates im Sammelbehälter mehr oder weniger drucklos. Nach einem weiteren Ausführungsbeispiel ist daher auf der Permeatablaufseite des RO-Moduls eine Druckerhöhungspumpe für das Permeat angeordnet, die zum einen zum Transport des Permeates und zur Einleitung des Permeates in ein Leitungssystem und zum anderen zur Förderung des Permeates durch die Aktivkohle-Filtereinheit dient. Die Druckerhöhung erfolgt dabei auf Permeatdruckwerte zwischen 3 und 10 bar, insbesondere in etwa 5 bar.While the full operating pressure applied by the pressure pump prevails on the concentrate or condensate side of the RO module, the permeate exits the RO module almost without pressure. Likewise, the storage of the permeate in the collection container takes place more or less without pressure. According to a further exemplary embodiment, a pressure booster pump for the permeate is therefore arranged on the permeate discharge side of the RO module, which serves on the one hand to transport the permeate and to introduce the permeate into a line system and on the other hand to promote the permeate through the activated carbon filter unit. The pressure is increased to permeate pressure values between 3 and 10 bar, in particular approximately 5 bar.

Der Reinigungswirkungsgrad der erfindungsgemäßen Anlage hängt unter anderem ganz wesentlich vom zulässigen Betriebsdruck des RO-Moduls ab. Grundsätzlich gilt, daß die Permeatausbeute um so höher ist, je größer der durch die Druckpumpe aufgebrachte Betriebsdruck ist. Dieser zulässige Druck ist jedoch insbesondere durch die mechanischen Eigenschaften der semipermeablen Membran und des RO-Moduls insgesamt begrenzt. Um dennoch den Gesamtwirkungsgrad der erfindungsgemäßen Reinigungsanlage bzw. des erfindungsgemäßen Verfahrens zu erhöhen, ist gemäß einem besonders bevorzugten Ausführungsbeispiel der Erfindung eine zuschaltbare Rückführungsleitung für das durch die semipermeable Membran zurückgehaltene und aus dem RO-Modul ausgetretene Konzentrat vor die Druckpumpe zur erneuten Durchströmung des RO-Moduls vorgesehen. Dies bedeutet mit anderen Worten, daß das aus dem RO-Modul austretende Konzentrat einem oder mehreren Umkehr-Osmose-Vorgängen unterzogen werden kann, wobei bei jedem dieser Umkehr-Osmose-Vorgänge eine stärkere Aufkonzentrierung des Konzentrates mit den organischen Verunreinigungen erfolgt. Aufgrund dieser Gestaltung und Verfahrensführung läßt sich in einfacher Weise ein Gesamtwirkungsgrad der Anlage von mehr als 90 % erzielen.The cleaning efficiency of the system according to the invention depends, among other things, very significantly on the permissible operating pressure of the RO module. Basically, the higher the operating pressure applied by the pressure pump, the higher the permeate yield. However, this permissible pressure is limited overall by the mechanical properties of the semipermeable membrane and the RO module. In order to nevertheless increase the overall efficiency of the cleaning system according to the invention or of the method according to the invention, according to a particularly preferred exemplary embodiment of the invention, a switchable return line for the concentrate retained by the semipermeable membrane and exiting from the RO module is in front of the pressure pump for renewed flow through the RO Module provided. In other words, this means that the concentrate emerging from the RO module is one or can be subjected to several reverse osmosis processes, with each of these reverse osmosis processes being more concentrated in the concentrate with the organic impurities. Due to this design and process management, an overall system efficiency of more than 90% can be achieved in a simple manner.

Eine Mehrfachreinigung des Konzentrates ist gemäß der Erfindung auch dadurch möglich, daß in einfacher Weise mehrere RO-Module in Reihe so hintereinander geschaltet werden, daß der Konzentratablauf jeweils eines vorgeschalteten RO-Moduls unmittelbar oder mittelbar in ein nachgeschaltetes RO-Modul mündet, wobei das Konzentrat dort erneut einem Reinigungsvorgang unterworfen wird.Multiple cleaning of the concentrate is also possible according to the invention in that a plurality of RO modules are connected in series in a simple manner so that the concentrate drain from an upstream RO module opens directly or indirectly into a downstream RO module, the concentrate there is again subjected to a cleaning process.

Insbesondere bei größeren Anlagen, das heißt Anlagen, bei denen größere Mengen an Brüdenkondensaten erfindungsgemäß aufgearbeitet bzw. gereinigt werden sollen, ist eine sogenannte Tannenbaumanordnung mehrerer RO-Module von Vorteil. Dabei sind zunächst in einer ersten Stufe mindestens zwei, vorzugsweise jedoch vier oder mehr RO-Module parallel angeordnet, die unter Aufteilung des Brüdenkondensatstroms von diesem durchlaufen werden. Die Konzentratabläufe der RO-Module dieser ersten Stufe können dann zusammengefaßt und einem oder mehreren RO-Modulen einer zweiten Stufe zur weiteren bzw. erneuten Reinigung zugeführt werden usw.. Die Anzahl der Stufen hängt letztendlich zum einen von der Menge des zu reinigenden Brüdenkondensates bzw. damit der Anzahl der RO-Module der ersten Stufe und zum anderen vom gewünschten Reinigungsgrad bzw. Wirkungsgrad der gesamten Anlage ab. Damit ist eine leichte und zuverlässige Auslegung der erfindungsgemäßen Anlage möglich.A so-called fir tree arrangement of a plurality of RO modules is advantageous in particular in larger systems, that is to say systems in which larger amounts of vapor condensates are to be worked up or cleaned according to the invention. In this case, at least two, but preferably four or more, RO modules are initially arranged in parallel in a first stage, and are passed through by the vapor condensate stream by dividing it. The concentrate drains of the RO modules of this first stage can then be combined and fed to one or more RO modules of a second stage for further or renewed cleaning, etc. The number of stages ultimately depends on the one hand on the amount of vapor condensate to be cleaned or thus the number of RO modules of the first stage and on the other hand the desired degree of cleaning or efficiency of the entire system. A simple and reliable design of the system according to the invention is thus possible.

Welche Art einer semipermeablen Membran in der erfindungsgemäßen Anlage bzw. im erfindungsgemäßen Verfahren Verwendung findet, hängt insbesondere von der Art der zu entfernenden organischen Verunreinigungen ab. Die kennzeichnenden Faktoren sind dafür insbesondere das Molekulargewicht, die Molekülgröße, die räumliche Struktur und die Ionogenität der Moleküle der Verunreinigungen. Zur Abtrennung insbesondere der in Sudhausbrüdenkondensaten anfallenden organischen Verunreinigungen hat sich durch Versuche die Verwendung einer hochvernetzten aromatischen Polyamid-Composite-Membran als zweckmäßig und vorteilhaft erwiesen. Eine derartige Membran wird beispielsweise üblicherweise zur Meerwasserentsalzung verwendet. Als eigentliches RO-Modul wird vorzugsweise ein spiralförmig gewundenes Wickelmodul verwendet, das einen textilen Träger aufweist, der die eigentliche semipermeable Membran trägt. Diese Gestaltung bietet in an sich bekannter Weise insbesondere eine ausreichende mechanische Festigkeit des RO-Moduls für Betriebsdrücke im Bereich bis zu 70 bar und mehr.Which type of semipermeable membrane is used in the system according to the invention or in the method according to the invention depends in particular on the type of organic impurities to be removed. The characteristic factors are in particular the molecular weight, the molecular size, the spatial structure and the ionogenicity of the molecules of the impurities. For separating in particular the brewhouse vapor condensates accruing organic impurities have proven to be expedient and advantageous through tests using a highly crosslinked aromatic polyamide composite membrane. Such a membrane is typically used for sea water desalination, for example. A spiral wound winding module is preferably used as the actual RO module, which has a textile carrier which carries the actual semipermeable membrane. This design offers, in a manner known per se, in particular sufficient mechanical strength of the RO module for operating pressures in the range up to 70 bar and more.

Die erfindungsgemäße Anlage und das erfindungsgemäße Verfahren sind im Brauereibereich unter anderem auch für die Reinigung und Aufbereitung des beim CO2-Wäscher aus dem Vorwäscher anfallenden Wassers geeignet.The plant and method according to the invention are also suitable in the brewery area, inter alia, for the cleaning and treatment of the water obtained in the CO 2 scrubber from the pre-scrubber.

Im folgenden ist die Erfindung anhand von lediglich Ausführungsbeispiele zeigenden Zeichnungen näher erläutert. Es zeigt

Fig. 1
ein Blockschaltbild einer Anlage gemäß der vorliegenden Erfindung mit einem RO-Modul; und
Fig. 2
ein Blockschaltbild einer erfindungsgemäßen Anlage mit mehreren RO-Modulen in Tannenbaumanordnung.
The invention is explained in more detail below with reference to drawings which show exemplary embodiments only. It shows
Fig. 1
a block diagram of a system according to the present invention with an RO module; and
Fig. 2
a block diagram of a system according to the invention with several RO modules in a fir tree arrangement.

Die in Fig. 1 dargestellte erfindungsgemäße Anlage weist zunächst einmal einen Zulauf 1 für das aus einem nicht dargestellten Pfannendunstkondensator stammende Brüdenkondensat auf. Der Zulauf 1 mündet in einen Vorlagebehälter 2, in dem das zu reinigende Kondensat zunächst gespeichert wird. Der Vorlagebehälter 2 kann dabei insbesondere die Funktion eines Pufferspeichers erfüllen, um einen kontinuierlichen Betrieb der erfindungsgemäßen Anlage zu gewährleisten. Mittels einer Vorlagepumpe 3 wird das zu reinigende Brüdenkondensat aus dem Vorlagebehälter 2 zur Druckpumpe 4 gefördert. Der durch die Vorlagepumpe 3 erzeugte Druck braucht dabei lediglich so hoch zu sein, daß ein sicherer Transport des zu reinigenden Brüdenkondensates zur Druckpumpe 4 sichergestellt ist.The system according to the invention shown in FIG. 1 first of all has an inlet 1 for the vapor condensate originating from a ladle vapor condenser, not shown. The inlet 1 opens into a storage container 2, in which the condensate to be cleaned is initially stored. The storage container 2 can in particular fulfill the function of a buffer store in order to ensure continuous operation of the system according to the invention. The vapor condensate to be cleaned is conveyed from the reservoir 2 to the pressure pump 4 by means of a feed pump 3. The pressure generated by the feed pump 3 need only be so high that a safe transport of the vapor condensate to be cleaned to the pressure pump 4 is ensured.

Mittels der Druckpumpe 4 wird der Druck des zu reinigenden Brüdenkondensates auf den für den Betrieb des RO-Moduls 5 notwendigen Betriebsdruck gebracht, der in der Regel zwischen 30 und 60 bar, beim dargestellten Ausführungsbeispiel insbesondere bei 40 bar, liegt.By means of the pressure pump 4, the pressure of the vapor condensate to be cleaned is brought to the operating pressure necessary for the operation of the RO module 5, which is generally between 30 and 60 bar, in particular 40 bar in the exemplary embodiment shown.

Im RO-Modul 5 ist, wie lediglich schematisch angedeutet ist, eine semipermeable Membran 6 angeordnet, die zur Reinigung des Brüdenkondensates durch einen Umkehr-Osmose-Vorgang dient. Die semipermeable Membran 6 teilt dabei das RO-Modul schematisch in zwei Kammern 7 und 8, wobei die Kammer 8 mit Wasser bzw. dem Permeat, d. h. mit einer Flüssigkeit geringer Konzentration insbesondere organischer Verunreinigungen, und die Kammer 7 mit dem zu reinigenden Brüdenkondensat, d. h. einer Flüssigkeit mit relativ hoher Konzentration organischer Verunreinigungen, gefüllt ist. Aufgrund des durch die Druckpumpe 4 aufgebrachten Druckes erfolgt ein Hindurchdiffundieren der Wasseranteile des Kondensates von der Kammer 7 durch die semipermeable Membran 6 in die Kammer 8.A semipermeable membrane 6, which serves to clean the vapor condensate by a reverse osmosis process, is arranged in the RO module 5, as is only indicated schematically. The semipermeable membrane 6 divides the RO module schematically into two chambers 7 and 8, the chamber 8 with water or the permeate, ie. H. with a liquid of low concentration, in particular organic contaminants, and the chamber 7 with the vapor condensate to be cleaned, i.e. H. a liquid with a relatively high concentration of organic impurities. Due to the pressure applied by the pressure pump 4, the water components of the condensate diffuse from the chamber 7 through the semipermeable membrane 6 into the chamber 8.

Aus dem RO-Modul bzw. der Kammer 8 des RO-Moduls wird das so gewonnene Permeat, d. h. mehr oder weniger reines Wasser, einem Sammelbehälter 9 zugeführt. Dabei erfolgt der Transport bzw. die Speicherung des Permeates nahezu drucklos. Über eine Druckerhöhungspumpe 10 wird das Permeat aus dem Sammelbehälter 9 zu einer Aktivkohle-Filtereinheit 11 und durch diese hindurch gefördert, wobei diese Aktivkohle-Filtereinheit 11 im wesentlichen mehr oder weniger lediglich eine Sicherheitseinrichtung für nicht bestimmungsgemäß in der semipermeablen Membran 6 zurückgehaltene Verunreinigungen darstellt.From the RO module or the chamber 8 of the RO module, the permeate thus obtained, i. H. more or less pure water, a collection container 9 supplied. The permeate is transported and stored almost without pressure. Via a pressure booster pump 10, the permeate is conveyed from the collecting container 9 to an activated carbon filter unit 11 and through it, this activated carbon filter unit 11 essentially representing more or less merely a safety device for impurities not retained in the semi-permeable membrane 6.

Nach dem Durchtritt durch die Aktivkohle-Filtereinheit 11 wird das Permeat über die Abgabeleitung 12 einer Wiederverwendung, gegebenenfalls nach Zwischenspeicherung, zugeführt. Die Druckerhöhungspumpe 10 dient zum einen zur Förderung des Permeates durch die Aktivkohle-Filtereinheit 11 und zum anderen zur Erhöhung des Druckes des Permeates auf einen Wert, mit dem dieses Permeat in ein entsprechendes Leitungssystem einspeisbar ist. Der Filtervorgang und das Einspeisen des Permeates in ein Leitungssystem erfolgen dabei vorzugsweise unter einem Druck zwischen 2 und 10 bar, insbesondere bei etwa 5 bar.After it has passed through the activated carbon filter unit 11, the permeate is fed via the discharge line 12 for reuse, if appropriate after intermediate storage. The pressure booster pump 10 serves on the one hand to convey the permeate through the activated carbon filter unit 11 and on the other hand to increase the pressure of the permeate to a value with which this permeate can be fed into a corresponding line system. The filtering process and feeding the permeate into one Line systems are preferably carried out under a pressure between 2 and 10 bar, in particular at about 5 bar.

Das Konzentrat, d. h. im wesentlichen die die organischen Verunreinigungen aufweisenden Bestandteile des Brüdenkondensates, wird aus der Kammer 7 des RO-Moduls über eine Ablaufleitung 13 abgeführt. Dabei kann das Konzentrat unmittelbar in eine lediglich schematisch dargestellte Kanalisation 14 abgegeben werden. Um insbesondere den Gesamtwirkungsgrad der erfindungsgemäßen Anlage zu erhöhen, weist die Anlage eine Rückführungsleitung 15 für das Konzentrat auf. Diese Rückführungsleitung 15 zweigt dabei vom Ablauf 13 ab und ist mittels nicht dargestellter Ventileinrichungen zu- oder abschaltbar. Die Rückführungsleitung 15 mündet zwischen der Vorlagepumpe 3 und der Druckpumpe 4 in den Strom des zu reinigenden Kondensates und ist dort mittels ebenfalls nicht dargestellter Ventileinrichtungen zu- oder abschaltbar. Wird nun die Rückführungsleitung 15 sowohl der Abführleitung 13 als auch dem Kondensatstrom zugeschaltet, erfolgt eine Wiedereinleitung des in der Kammer 7 angefallenen Konzentrates in den Reinigungsstrom und damit eine erneute bzw. weitere Reinigung des Kondensates bzw. des Konzentrates. Durch wiederholte Rückführung des in der Kammer 7 angefallenen Konzentrates in den Reinigungskreislauf kann dabei in einfacher Weise ein Gesamtwirkungsgrad der Anlage von mehr als 90 % erreicht werden.The concentrate, i.e. H. essentially the components of the vapor condensate containing the organic impurities are discharged from the chamber 7 of the RO module via a drain line 13. The concentrate can be discharged directly into a sewer system 14, which is only shown schematically. In order in particular to increase the overall efficiency of the system according to the invention, the system has a return line 15 for the concentrate. This return line 15 branches off from the outlet 13 and can be switched on or off by means of valve devices (not shown). The return line 15 opens between the feed pump 3 and the pressure pump 4 in the flow of the condensate to be cleaned and can be switched on or off there by means of valve devices, also not shown. If the return line 15 is now connected to both the discharge line 13 and the condensate stream, the concentrate accumulated in the chamber 7 is reintroduced into the cleaning stream and thus the condensate or the concentrate is cleaned again or further. By repeatedly returning the concentrate accumulated in chamber 7 to the cleaning circuit, an overall system efficiency of more than 90% can be achieved in a simple manner.

Das in Fig. 2 dargestellte Ausführungsbeispiel einer erfindungsgemäßen Anlage zur Reinigung von Brüdenkondensaten entspricht in seinem grundsätzlichen Aufbau der Anlage gemäß Fig. 1. Das singuläre RO-Modul der Anlage nach Fig. 1 ist jedoch ersetzt durch eine tannenbaumartige Anordnung 23 aus sieben im wesentlichen gleichen RO-Modulen 16, 17, 18, 19, 20, 21 und 22, die in drei nacheinander, bezogen auf die Durchflußrichtung des zu reinigenden Kondensates, plazierten Stufen I, II und III angeordnet sind.The exemplary embodiment of an installation according to the invention for cleaning vapor condensates shown in FIG. 2 corresponds in its basic structure to the installation according to FIG. 1 . The singular RO module of the system according to FIG. 1 is, however, replaced by a fir tree-like arrangement 23 of seven essentially identical RO modules 16, 17, 18, 19, 20, 21 and 22, which are arranged in three in succession, based on the flow direction of the condensate to be cleaned, placed stages I, II and III are arranged.

Die erste Stufe I weist dabei vier parallel nebeneinander angeordnete RO-Module 16, 17, 18 und 19 auf, auf die sich der von der Druckpumpe 4 geförderte Strom der Brüdenkondensate verteilt. Bereits dadurch wird die Kapazität der gesamten Anlage, die im wesentlichen durch die Durchflußleistung der RO-Module bestimmt wird, verglichen mit der Anlage nach Fig. 1 wesentlich erhöht.The first stage I has four RO modules 16, 17, 18 and 19 arranged in parallel next to one another, on which the flow of the vapor condensates conveyed by the pressure pump 4 is based distributed. This alone increases the capacity of the entire system, which is essentially determined by the flow rate of the RO modules, compared to the system according to FIG. 1 .

In der zweiten Stufe II sind zwei RO-Module 20, 21 ebenfalls parallel nebeneinander angeordnet. Die Konzentratabläufe der RO-Module 16, 17 bzw. 18, 19 der ersten Stufe I münden dabei unmittelbar in das RO-Modul 20 bzw. 21 der zweiten Stufe II und werden dort einem erneuten Reinigungs- bzw. Filtervorgang unterzogen. In prinzipiell gleicher Weise münden die Konzentratabläufe der RO-Module 20, 21 der zweiten Stufe II in das RO-Modul 22 der dritten Stufe III. Nach dort erfolgter abermaliger Reinigung wird das Konzentrat über die Leitung 13 schließlich in die Kanalisation 14 abgegeben oder, falls gewünscht, über die Rückführungsleitung 15 erneut zur weiteren Reinigung in die RO-Modulanordnung 23 geführt. Das durch die RO-Module hindurchtretende Permeat wird jeweils unmittelbar über die Aktivkohle-Filtereinheit in den Sammelbehälter zur weiteren Verwendung beispielsweise als Brauwasser gegeben. Durch diese tannenbaumartige RO-Modulanordnung 23 ist in einfacher und leichter Weise ein hoher Reinigungswirkungsgrad der Anlage zu erreichen.In the second stage II, two RO modules 20, 21 are also arranged side by side in parallel. The concentrate drains of the RO modules 16, 17 and 18, 19 of the first stage I open directly into the RO module 20 and 21 of the second stage II, where they are subjected to a renewed cleaning or filtering process. In principle the same way, the concentrate drains of the RO modules 20, 21 of the second stage II open into the RO module 22 of the third stage III. After repeated cleaning there, the concentrate is finally discharged via the line 13 into the sewage system 14 or, if desired, again via the return line 15 for further cleaning into the RO module arrangement 23. The permeate passing through the RO modules is in each case passed directly via the activated carbon filter unit into the collection container for further use, for example as brewing water. With this fir tree-like RO module arrangement 23, a high cleaning efficiency of the system can be achieved in a simple and easy manner.

Claims (20)

Anlage zur Reinigung von insbesondere bei der Bierherstellung anfallenden Brüdenkondensaten,
gekennzeichnet durch
mindestens eine Druckpumpe (4) zur Druckbeaufschlagung des zu reinigenden Brüdenkondensates und mindestens ein eine semipermeable Membran (6) aufweisendes RO-Modul (5; 16 - 22), durch das das Brüdenkondensat mittels der Druckpumpe (4) unter Trennung in Permeat und Konzentrat förderbar ist, wobei ferner eine Ablaufleitung (13) für das Konzentrat zur mittelbaren oder unmittelbaren Ableitung in die Kanalisation (14) vorgesehen und das gereinigte Permeat zur Wiederverwendung sammelbar ist.Plant for the purification of vapor condensates, particularly those produced in beer production,
characterized by
at least one pressure pump (4) for pressurizing the vapor condensate to be cleaned and at least one RO module (5; 16 - 22) having a semipermeable membrane (6), through which the vapor condensate can be conveyed by means of the pressure pump (4) with separation into permeate and concentrate A drain line (13) for the concentrate for indirect or direct discharge into the sewage system (14) is also provided, and the cleaned permeate can be collected for reuse. Anlage nach Anspruch 1,
gekennzeichnet durch
einen in Durchflußrichtung vor der Druckpumpe (4) angeordneten Vorlagebehälter (2) zur Speicherung des zu reinigenden Brüdenkondensates.System according to claim 1,
characterized by
a storage container (2) arranged upstream of the pressure pump (4) for storing the vapor condensate to be cleaned. Anlage nach Anspruch 2,
gekennzeichnet durch
eine zwischen dem Vorlagebehälter (2) und der Druckpumpe (4) angeordnete Vorlagepumpe (3) zur Förderung des zu reinigenden Brüdenkondensates aus dem Vorlagebehälter (2) zur Druckpumpe (4).System according to claim 2,
characterized by
a feed pump (3) arranged between the feed tank (2) and the pressure pump (4) for conveying the vapor condensate to be cleaned from the feed tank (2) to the pressure pump (4). Anlage nach einem der Ansprüche 1 bis 3,
gekennzeichnet durch
einen auf der Permeatablaufseite des RO-Moduls (5) angeordneten Sammelbehälter (9) für das durch die semipermeable Membran (6) hindurchgetretene Permeat.System according to one of claims 1 to 3,
characterized by
a collecting container (9) arranged on the permeate discharge side of the RO module (5) for the permeate which has passed through the semipermeable membrane (6). Anlage nach einem der Ansprüche 1 bis 4,
gekennzeichnet durch
mindestens eine auf der Permeatablaufseite des RO-Moduls (5) angeordnete Aktivkohle-Filtereinheit (11), die vom Permeat durchströmbar ist.System according to one of claims 1 to 4,
characterized by
at least one activated carbon filter unit (11) arranged on the permeate discharge side of the RO module (5), through which the permeate can flow. Anlage nach einem der Ansprüche 1 bis 5,
gekennzeichnet durch
mindestens eine auf der Permeatablaufseite des RO-Moduls (5) angeordnete Druckerhöhungspumpe (10) für das Permeat.System according to one of claims 1 to 5,
characterized by
at least one pressure booster pump (10) for the permeate arranged on the permeate discharge side of the RO module (5). Anlage nach Anspruch 6,
dadurch gekennzeichnet,
daß die Druckerhöhungspumpe (10), bezogen auf die Strömungsrichtung des Permeats, nach dem Sammelbehälter (9) angeordnet ist.System according to claim 6,
characterized by
that the pressure booster pump (10), based on the flow direction of the permeate, is arranged after the collecting container (9). Anlage nach Anspruch 6 oder 7,
dadurch gekennzeichnet,
daß die Aktivkohle-Filtereinheit (11), bezogen auf die Strömungsrichtung des Permeats, nach der Druckerhöhungspumpe (10) angeordnet ist.System according to claim 6 or 7,
characterized by
that the activated carbon filter unit (11), based on the flow direction of the permeate, is arranged after the pressure booster pump (10). Anlage nach einem der Ansprüche 1 bis 8,
gekennzeichnet durch
eine zuschaltbare Rückführungsleitung (15) für das durch die semipermeable Membran (6) zurückgehaltene und aus dem RO-Modul (5) ausgetretene Konzentrat vor die Druckpumpe (4) zur erneuten Durchströmung des RO-Moduls (5).System according to one of claims 1 to 8,
characterized by
a switchable return line (15) for the concentrate retained by the semipermeable membrane (6) and exiting from the RO module (5) in front of the pressure pump (4) for fresh flow through the RO module (5). Anlage nach einem der Ansprüche 1 bis 9,
dadurch gekennzeichnet,
daß das RO-Modul (5) ein vorzugsweise spiralförmig gewundenes Wickelmodul mit einem textilen Träger und der eigentlichen semipermeablen Membran (6) aufweist.System according to one of claims 1 to 9,
characterized by
that the RO module (5) has a preferably spirally wound winding module with a textile carrier and the actual semipermeable membrane (6). Anlage nach einem der Ansprüche 1 bis 10,
dadurch gekennzeichnet,
daß die semipermeable Membran (6) durch eine hochvernetzte aromatische Polyamid-Composite-Membran gebildet wird.Installation according to one of claims 1 to 10,
characterized by
that the semipermeable membrane (6) is formed by a highly cross-linked aromatic polyamide composite membrane. Anlage nach einem der Ansprüche 1 bis 11,
dadurch gekennzeichnet,
daß zwei oder mehr RO-Module (5) in Reihe hintereinander so angeordnet sind, daß der Konzentratablauf des jeweils vorgeschalteten RO-Moduls mittelbar oder unmittelbar in das jeweils folgende RO-Modul mündet.Installation according to one of claims 1 to 11,
characterized by
that two or more RO modules (5) are arranged in series one behind the other so that the concentrate drain of the upstream RO module opens directly or indirectly into the following RO module. Anlage nach einem der Ansprüche 1 bis 12,
dadurch gekennzeichnet,
daß eine Vielzahl von RO-Modulen (16 - 22) tannenbaumartig in Stufen (I, II, III) nacheinander angeordnet sind, wobei die Anzahl der RO-Module von Stufe zu Stufe in Durchflußrichtung gesehen abnimmt und die Konzentratabläufe der RO-Module (16 - 22) der jeweils vorgeschalteten Stufe unmittelbar oder mittelbar in mindestens ein RO-Modul der jeweils nachgeschalteten Stufe münden.System according to one of claims 1 to 12,
characterized by
that a multiplicity of RO modules (16-22) are arranged in a fir tree-like manner in stages (I, II, III), the number of RO modules decreasing from stage to stage in the direction of flow and the concentrate processes of the RO modules (16 - 22) of the upstream stage lead directly or indirectly into at least one RO module of the downstream stage. Verfahren zur Reinigung von bei der Bierherstellung anfallenden Brüdenkondensaten,
gekennzeichnet durch
folgende Verfahrensschritte: - Erhöhung des Druckes des Kondensates mittels einer Druckpumpe (4); - Förderung des unter Druck stehenden Kondensates an die semipermeable Membran (6) mindestens eines RO-Moduls (5); - Ableitung des durch die semipermeable Membran (6) abgehaltenen Konzentrates mittelbar oder unmittelbar in die Kanalisation (14); und - Ableitung des durch die semipermeable Membran (6) hindurchgetretenen Permeates zur Wiederverwendung. Process for cleaning vapor condensates from beer production,
characterized by
following process steps: - Increasing the pressure of the condensate by means of a pressure pump (4); - conveying the pressurized condensate to the semipermeable membrane (6) of at least one RO module (5); - Deriving the concentrate held by the semipermeable membrane (6) directly or indirectly into the sewer system (14); and - Deriving the permeate that has passed through the semipermeable membrane (6) for reuse. Verfahren nach Anspruch 14,
dadurch gekennzeichnet,
daß der durch die Druckpumpe (4) erhöhte Druck des Kondensates zwischen 30 und 60 bar, insbesondere 40 bar beträgt.The method of claim 14
characterized by
that the pressure of the condensate increased by the pressure pump (4) is between 30 and 60 bar, in particular 40 bar. Verfahren nach Anspruch 14 oder 15,
dadurch gekennzeichnet,
daß vor der Erhöhung des Druckes mittels der Druckpumpe (4) das zu reinigende Brüdenkondensat in einem Vorlagebehälter (2) gespeichert oder gesammelt und von dort mittels einer Vorlagepumpe (3) zur Druckpumpe (4) gefördert wird.A method according to claim 14 or 15,
characterized by
that before the pressure is increased by means of the pressure pump (4), the vapor condensate to be cleaned is stored or collected in a storage container (2) and is conveyed from there to the pressure pump (4) by means of a feed pump (3). Verfahren nach einem der Ansprüche 14 bis 16,
dadurch gekennzeichnet,
daß das an der semipermeablen Membran (6) zurückgehaltene Konzentrat zur Druckpumpe (4) zurückgeführt und wieder dem RO-Modul (5) zur erneuten Reinigung zugeleitet wird.Method according to one of claims 14 to 16,
characterized by
that the concentrate retained on the semipermeable membrane (6) is returned to the pressure pump (4) and fed back to the RO module (5) for renewed cleaning. Verfahren nach einem der Ansprüche 14 bis 17,
dadurch gekennzeichnet,
daß das an der semipermeablen Membran (6) zurückgehaltene Konzentrat mindestens einem nachgeschalteten weiteren RO-Modul zur erneuten Reinigung zugeleitet wird.Method according to one of claims 14 to 17,
characterized by
that the concentrate retained on the semipermeable membrane (6) is fed to at least one downstream RO module for renewed cleaning. Verfahren nach einem der Ansprüche 14 bis 18,
dadurch gekennzeichnet,
daß das Permeat vor seiner Wiederverwendung einem Filtervorgang, insbesondere in einem Aktivkohlefilter (11), unterzogen wird.Method according to one of claims 14 to 18,
characterized by
that the permeate is subjected to a filtering process, in particular in an activated carbon filter (11), before it is reused. Verfahren nach Anspruch 19,
dadurch gekennzeichnet,
daß der Filtervorgang unter einem Permeatdruck zwischen 3 und 10 bar, insbesondere 5 bar, erfolgt.Method according to claim 19,
characterized by
that the filtering process takes place under a permeate pressure between 3 and 10 bar, in particular 5 bar.
EP96107490A 1995-05-12 1996-05-10 Apparatus and method of cleaning vapour condensate produced during the boiling of the wort in the beer production Expired - Lifetime EP0742283B1 (en)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
DE19516969 1995-05-12
DE19516969A DE19516969A1 (en) 1995-05-12 1995-05-12 Plant and method for cleaning vapor condensates from wort boiling during beer production

Publications (3)

Publication Number Publication Date
EP0742283A2 true EP0742283A2 (en) 1996-11-13
EP0742283A3 EP0742283A3 (en) 2001-04-18
EP0742283B1 EP0742283B1 (en) 2004-08-11

Family

ID=7761451

Family Applications (1)

Application Number Title Priority Date Filing Date
EP96107490A Expired - Lifetime EP0742283B1 (en) 1995-05-12 1996-05-10 Apparatus and method of cleaning vapour condensate produced during the boiling of the wort in the beer production

Country Status (3)

Country Link
EP (1) EP0742283B1 (en)
AT (1) ATE273380T1 (en)
DE (2) DE19516969A1 (en)

Cited By (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP0876840A1 (en) * 1997-05-05 1998-11-11 ALUMINIUM RHEINFELDEN GmbH Method and apparatus for recovering, concentrating or reducing of vaporous and/or gaseous materials out of a vaporous and/or gaseous mixture of substances
EP0878228A1 (en) * 1997-05-05 1998-11-18 ALUMINIUM RHEINFELDEN GmbH Method and apparatus for recovering, concentrating or reducing of vapors and/or gaseous materials out of a vaporous and/or gaseous mixture of substances
US6328893B1 (en) 1997-04-03 2001-12-11 Frings Recycling-Anlagen Gmbh & Co. Kg Method of processing waste water, in particular from malt factories and breweries

Families Citing this family (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE4442393C1 (en) * 1994-11-29 1995-09-21 Umweltkompatible Prozestechnik Separation of organic matter from wort vapour condensation
DE19757138C1 (en) * 1997-12-20 1998-10-22 Michael Eumann Beer wort condensate processing apparatus

Citations (10)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4801375A (en) * 1987-02-17 1989-01-31 Cuno Incorporated Water vending system
DE3925343A1 (en) * 1989-07-31 1991-02-07 Brautechnische Anlagen Gmbh Treating hot brewery plant emissions - by condensn. and cyclone separator followed by adsorption
US5017291A (en) * 1990-10-24 1991-05-21 Semler Industries, Inc. Process for recycling and reconstituting flexographic inks
US5122233A (en) * 1989-04-24 1992-06-16 Charles Zampieri Apparatus for the treatment of mixture of brines and contaminated mineral salts
DE4121382C1 (en) * 1991-06-28 1992-09-17 Degussa Ag, 6000 Frankfurt, De Hexa:methylene:tetramine prodn. using formaldehyde stream from methanol oxidn. - comprises reacting formaldehyde with ammonia, in aq. phase with water removal at reduced pressure
EP0530766A1 (en) * 1991-09-03 1993-03-10 Albemarle Corporation Bromide separation and concentration using nanofiltration
US5244579A (en) * 1992-10-09 1993-09-14 Zenon Environmental Inc. Transportable reverse osmosis water purification unit
DE4302319A1 (en) * 1992-05-21 1993-11-25 Deutsche Aerospace Airbus Process and arrangement for the treatment of waste water, especially in aircraft
DE4442393C1 (en) * 1994-11-29 1995-09-21 Umweltkompatible Prozestechnik Separation of organic matter from wort vapour condensation
EP0709130A1 (en) * 1994-10-12 1996-05-01 Toray Industries, Inc. Apparatus and method for multistage reverse osmosis separation

Patent Citations (11)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4801375A (en) * 1987-02-17 1989-01-31 Cuno Incorporated Water vending system
US5122233A (en) * 1989-04-24 1992-06-16 Charles Zampieri Apparatus for the treatment of mixture of brines and contaminated mineral salts
DE3925343A1 (en) * 1989-07-31 1991-02-07 Brautechnische Anlagen Gmbh Treating hot brewery plant emissions - by condensn. and cyclone separator followed by adsorption
US5017291A (en) * 1990-10-24 1991-05-21 Semler Industries, Inc. Process for recycling and reconstituting flexographic inks
DE4121382C1 (en) * 1991-06-28 1992-09-17 Degussa Ag, 6000 Frankfurt, De Hexa:methylene:tetramine prodn. using formaldehyde stream from methanol oxidn. - comprises reacting formaldehyde with ammonia, in aq. phase with water removal at reduced pressure
EP0530766A1 (en) * 1991-09-03 1993-03-10 Albemarle Corporation Bromide separation and concentration using nanofiltration
DE4302319A1 (en) * 1992-05-21 1993-11-25 Deutsche Aerospace Airbus Process and arrangement for the treatment of waste water, especially in aircraft
US5244579A (en) * 1992-10-09 1993-09-14 Zenon Environmental Inc. Transportable reverse osmosis water purification unit
EP0709130A1 (en) * 1994-10-12 1996-05-01 Toray Industries, Inc. Apparatus and method for multistage reverse osmosis separation
DE4442393C1 (en) * 1994-11-29 1995-09-21 Umweltkompatible Prozestechnik Separation of organic matter from wort vapour condensation
DE19544336A1 (en) * 1994-11-29 1996-06-27 Upt Ges Fuer Umweltkompatible Processing waste waters, e.g. from beer prodn.

Cited By (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US6328893B1 (en) 1997-04-03 2001-12-11 Frings Recycling-Anlagen Gmbh & Co. Kg Method of processing waste water, in particular from malt factories and breweries
EP0876840A1 (en) * 1997-05-05 1998-11-11 ALUMINIUM RHEINFELDEN GmbH Method and apparatus for recovering, concentrating or reducing of vaporous and/or gaseous materials out of a vaporous and/or gaseous mixture of substances
EP0878228A1 (en) * 1997-05-05 1998-11-18 ALUMINIUM RHEINFELDEN GmbH Method and apparatus for recovering, concentrating or reducing of vapors and/or gaseous materials out of a vaporous and/or gaseous mixture of substances

Also Published As

Publication number Publication date
DE19516969A1 (en) 1996-11-14
DE59611052D1 (en) 2004-09-16
EP0742283B1 (en) 2004-08-11
EP0742283A3 (en) 2001-04-18
ATE273380T1 (en) 2004-08-15

Similar Documents

Publication Publication Date Title
DE3303571A1 (en) METHOD FOR PRODUCING AETHANOL
EP2167222B1 (en) Method for processing cleaning fluids
DE19630089C1 (en) Process and assembly treats waste water and tensides separately by nano-filtration
DE102014112240A1 (en) Process for the treatment of process water
DE69937046T2 (en) BIG PIPE ASSEMBLY FOR REVERSE OSMOSIS
EP2292562B1 (en) Method and assembly for filtering water, in particular ultrafiltration method
EP0824503A1 (en) Waste water treatment process for producing high yields of drinking water
DE102014215405A1 (en) Process for wastewater treatment of oily wastewater and wastewater treatment plant
AT502037B1 (en) METHOD FOR CLEANING OBJECTS AND CLEANING SYSTEM
EP1832333A1 (en) Method for recovery of impure fluids
DE3041209A1 (en) METHOD FOR THE TREATMENT OF IN PARTICULAR NITRATE-CONTAINING WATER
EP0742283B1 (en) Apparatus and method of cleaning vapour condensate produced during the boiling of the wort in the beer production
EP0338043A1 (en) Process and plant for clarifying liquids, in particular raw juice
DE3513940A1 (en) Unit for the treatment of laundry water
EP0491015B1 (en) Process for rinsing the filter module of a device for purifying liquids
WO2018087384A1 (en) Treatment of wastewater to obtain drinking water by means of ozone
EP1805151A1 (en) Method for the treatment of triazine-containing water of a melamine plant
DE202007015082U1 (en) Plant for cleaning water
EP1265819B1 (en) Method and device for effluent treatment
DE202009017790U1 (en) Wastewater treatment plant for the treatment of waste water from oil crops and grain processing
DE202019001503U1 (en) 3D-Filtration-ULW Ultrafiltration of the circulating water from hybrid recooling plants and other cooling plants with circulating water
AT410314B (en) METHOD AND DEVICE FOR THE TREATMENT OF ORGANICALLY LOADED WASTE WATER
DE19502440A1 (en) Purifying waste water esp. water from photographic industry, electroplating, eloxal process or neutralisation
EP0567866A1 (en) Treating of waste water from printing plants
WO2003091164A1 (en) Method and device for purifying drinking water using a chlorine-resistant nanofiltration membrane

Legal Events

Date Code Title Description
PUAI Public reference made under article 153(3) epc to a published international application that has entered the european phase

Free format text: ORIGINAL CODE: 0009012

AK Designated contracting states

Kind code of ref document: A2

Designated state(s): AT BE DE ES FR GB IT NL

RAP1 Party data changed (applicant data changed or rights of an application transferred)

Owner name: LENZ, AUGUST

Owner name: LENZ, BERNHARD

PUAL Search report despatched

Free format text: ORIGINAL CODE: 0009013

AK Designated contracting states

Kind code of ref document: A3

Designated state(s): AT BE DE ES FR GB IT NL

17P Request for examination filed

Effective date: 20011016

RAP1 Party data changed (applicant data changed or rights of an application transferred)

Owner name: HRCH. HUPPMANN GMBH

RIN1 Information on inventor provided before grant (corrected)

Inventor name: LENZ, AUGUST

Inventor name: LENZ, BERNHARD

17Q First examination report despatched

Effective date: 20030203

GRAP Despatch of communication of intention to grant a patent

Free format text: ORIGINAL CODE: EPIDOSNIGR1

GRAS Grant fee paid

Free format text: ORIGINAL CODE: EPIDOSNIGR3

GRAA (expected) grant

Free format text: ORIGINAL CODE: 0009210

AK Designated contracting states

Kind code of ref document: B1

Designated state(s): AT BE DE ES FR GB IT NL

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: NL

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20040811

Ref country code: IT

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRE;WARNING: LAPSES OF ITALIAN PATENTS WITH EFFECTIVE DATE BEFORE 2007 MAY HAVE OCCURRED AT ANY TIME BEFORE 2007. THE CORRECT EFFECTIVE DATE MAY BE DIFFERENT FROM THE ONE RECORDED.SCRIBED TIME-LIMIT

Effective date: 20040811

Ref country code: GB

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20040811

Ref country code: FR

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20040811

REG Reference to a national code

Ref country code: GB

Ref legal event code: FG4D

Free format text: NOT ENGLISH

REF Corresponds to:

Ref document number: 59611052

Country of ref document: DE

Date of ref document: 20040916

Kind code of ref document: P

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: ES

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20041122

NLV1 Nl: lapsed or annulled due to failure to fulfill the requirements of art. 29p and 29m of the patents act
GBV Gb: ep patent (uk) treated as always having been void in accordance with gb section 77(7)/1977 [no translation filed]

Effective date: 20040811

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: AT

Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES

Effective date: 20050510

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: BE

Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES

Effective date: 20050531

PLBE No opposition filed within time limit

Free format text: ORIGINAL CODE: 0009261

STAA Information on the status of an ep patent application or granted ep patent

Free format text: STATUS: NO OPPOSITION FILED WITHIN TIME LIMIT

PGFP Annual fee paid to national office [announced via postgrant information from national office to epo]

Ref country code: DE

Payment date: 20050720

Year of fee payment: 10

26N No opposition filed

Effective date: 20050512

EN Fr: translation not filed
EN Fr: translation not filed
BERE Be: lapsed

Owner name: HRCH. *HUPPMANN G.M.B.H.

Effective date: 20050531

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: DE

Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES

Effective date: 20061201

BERE Be: lapsed

Owner name: HRCH. *HUPPMANN G.M.B.H.

Effective date: 20050531